Oil fractionation



March 7, 1933- J. s. WALLIS OIL FRACTIONATION Filed Jan. 14, 1950 2 Sheets-Sheet 2 Patented M.. y7, i935 .torna vnr. wams, or anw Yoan, n'. Y., AssyIGNon ro FOSTER WHEELER.

RATION, NEW YORK, N. Y., A CORPORATION OF YORK @EL FBAC'QIONATION My invention relates'to oil fractionation. More particularly, my invention relates to apparatus for fractionating oil. Still more particularly, my invention relates to fraction ating towers in which condensation is pro-A duced by redux circulation and from which l a plurality of side streams arewithdrawn.

lin tractionating towers of the type where- `in condensation is obtained by'reflux and lo from which a plurality of side streams are withdrawn, it is .common practice to pro- 4vide bubble trays of similar construction. The trays are made to have the same size vapor openings and to have the same velocity of flow of liquid horizontally over them at all places in the tower. ln towers of this type the amount of liquid flowing down in different portions ofthe tower is not uniform. Consequently, the use of similar trays throughout a tower results in variation of velocity of flow of liquid over the trays.

lt is the principal object of the present invention to provide structure whereby uniform or more or less equalized velocity of flow of liquid oil over bubble trays is obtained in a tower wherein the quantity of downiowing liquid is dierent ordiderent zones or sections of the tower. ln particular,

ll aim to improve towers of the type above re- Sa erred to, although the inventlon is applicable to `.various kinds of structures.`

Assume that-stock oil is heated in a still and introduced into a fractionating tower, the conditions beingsuch that 90 percent of t5 the oil is in the vapor phase at the point of introduction of the oilinto the tower. Assume also that percent of this vapor is withdrawn as vapor at the top of the tower, the remainder being withdrawn as conden- Q@ 4sate atene ormore intermediate oints. It ,will be seen that the condensing e ect of the tower must take care 'of the 60 percent which is liquefied in the tower. Since the condensation reslts (disregarding radiation) from 43 the introduction into the towed' of liquid oil,`

. it will be seen that the 'quantity of liquid Aoil introduced for condensing purposes must be large to take care of the latent heat o vaporization of the oil which is liquefied inthe tower. rlhe result is that a. large quantity 'of liquid Hows over the upper trays of the tower and the quantity of liquid' lowing over trays diminishes to a high degree at respective y lower points of the tower due to` the condensation and the removal of fractions at the intermediate points of withdrawal.. The reflux liquid being of low boiling point vaporizes in the upper art of the tower and there is thus a relatlvely large a undesirable'since both slow flow of liquid and h ightemperature tend to increase precipitation. It will be seen that if there is any free carbon in the oil it is most likely to separate out from the liquid and cake on a .tray at the point of highest temperature and slow- 'est flow. It `will thus be seen that theseI two factors, soR to speak, aggravate each other. To overcome this disadvantage, I propose to constructrthe bubble trays so that the velocity of flow of liquid is made more uniform` than `has been prior practice. At the 4same time, I construct the trays so that the area 'for passage of vapor is not changed.

Since the volumev of vapor (oil plus steam) may be considered uniform throughout the tower forthe present consideration, it will be seen that this volume will determine the Asize of traysfor the best eciency." Using at y a cylindrical tower, which/.is best suited for practical purposes, the area of trays 'tor liquid iow is consequently the same for diiiie'r` ent trays if the whole surface or a given percentage of surface `oi? the tray is usedy for liquid fiow. Consequently, .I attain my object by maintaining constant area of gas and liquid contact on the trays and increase the length of the path of travel for oil. as the amount of liquid for a given tray decreases per unit of time.

The invention w1ll be explained with reffi erence to the accompanying drawings showing more or less diagrammatlcally one form of apparatus embodying the invention, and consideration of the following specification will show more clearly the nature, objects and advantages of the invention.

lln the drawings: Y

Fig. 1 shows more or less diagrammatically an oil fractionating tower;

Fig. 2 isa diagram of quantities of ,liquid in different parts of the tower;

Fig. 3 is a diagram showing proportion of steam volume to oil volume;

Fig. 4 is a more or less diagrammatic crosssectional view of the trays in the upper part of the tower shown in Fig.4 1;

Fig. 5 is a similar cross-sectional view showing the trays in the intermediate portion of the tower;

Fig. 6 is a cross-sectional view of a portion i of the tower just above the oil supply;

Fig. 7 is a cross-sectional view of the lower part of the tower;

. Figs. 4 to 7 inclusive are shown opposite portions of the tower containing the trays therein represented respectively;

Fig. 8 is a more detailed view of a portion of the tower;

Fig. 9 is a cross-sectional view taken on the line 9-9 of Fig. 8 and on the line 9-9 of Fig. 1; and

Fig. 10 is a cross-sectional view taken on the line 10-10 of Fig. 8 and on the line 10- 10 of Fig. 1.

'llhe tower comprises a shell 10 -which is vertically disposed and cylindrical and preferably of uniformdiameter except for the base portion thereof. The tower contains a series of horizontal bubble trays indicated generally at 12, which trays may be of various kinds, trays with elongated ports being shown forsake of illustration.

Oil to be fractionated in the tower 10 is supplied from a still or heater 13 by means of a conduit 14. Vapor is withdrawn from the) upper part of the tower through conduit 15, is condensed in a condenser 16 and a portion of this oil Ais pumped back through conduit 17 and pump 18 into the top of the tower above the upper tray, constituting the revflux which serves as a condensing medium within the tower. Steam is supplied from the heater 13 through conduit 19 and the branch. conduits 20, 21, 22 and 23 to various vertically disposed portions of the tower as shown in Fig. 1. Intermediate fractions are withdrawn from the tower through conduits 24', 24 and 25 and the bottoms are withdrawn through conduit 26.

rlhe redux oil flows downwardly from tray to tray. Downflow connections are provided as shown in Fig. 8 and indicated generally by reference character 27. Each tray carries a body of liquid thereon, the'height of which yis determined by the height of an overflow edge 28 or other similar level maintaining device. 'llhe elongated ports 29 may be a have raised sides to prevent liquid from flowing down through the same and have caps 30 thereover having down-turned edges which extend into the body of liquid oil on the tray. Vapors passing upwardly through the tower are forced to pass through the y ports 29 and through liquid on the trays.

, low the scrubbing section. An internal conduit 34 serves for upward flow of oil vapor past the scrubbing section. The steam is introduced into the scrubbing section as through conduit 21 and the fraction is withdrawn therefrom as through the conduit 24. l do not claim as my invention these details of bubble tray construction or the structure of the scrubbing section. For further information as to these features reference may be had to a copending application of John Primrose and Harry R. Swanson, Serial No. 106,866, filed lMay 5th, 1926, which has matured into Patent No. 1,893,906, granted January 10, 1933.

Fig. 2 is a diagram showing roughly the amount of liquid in the tower at different portions of the tower, under an assumed state of conditions substantially of 36% voverhead vapor and three side streams of 36%, 12%

. and 6% respectively. rlhe diagram is merely by Way of example, but is typical of the general relation of quantities of liquid in a tower of this kind. The reflux liquid passing through conduit 17 is a big percentage of the total liquid inthe tower. Consequently there is a large amount of liquid flowing over the trays in the upper part of the tower. Much of this liquid reevaporates in the upper part of the tower and as a result of operation 1ncluding the withdrawal of a fraction through conduit 24', the quantity of liquid is so reduced that the quantity flowing over the traysnbetween the withdrawal conduits 24 and 24 may be one-third the quantity 1n the upper part of the tower. 1 Slmilarly the amount of liquid flowing over the trays below withdrawal conduit 24 and above the oil inlet 14 is much reduced. rlhere is condensation at all points of thi J towerand so there difference of quantities on all trays, but in general the change of quantity at the place of withdrawal may be as shown in Fig. 2.

lf the same kind of bubble tray is used in all parts of the tower, with the same number of ports and the same size of ports, the flow across' the trays is of much higher velocity at thertop plate, and, in accordance with the assumed conditions, the velocity of liquid across the tray near the vapor inlet 14 may be one-sixth or less of the velocity on the uppermost tray. -The lowest tray of those now referred to isin the highest temperature zoneand the velocity of liquid thereon should be high to eliminate the possibility of deposition or precipitation.

In order to equalize, so faras possible, the rate ofl fiowjof liquid over the trays, I propose to use trays of uniform gas passage area but constructed differently for different parts of the tower so as to vary-the cross-sectional area of the path of liquid flow in order to l `substantially prevent reduction of liquid flow velocity due to the lesser quantities of liquid in lower portions of the tower, respectively. My planl for accomplishing this object is shown more or less diagrammatically in Figs. 4, 5 and 6.

Referring to Fig. 3, it is to be noted 'that the vapor volume throughout the fractionating tower above the inlet is practically uniform. 'lihis volumeis probably ten. to fifteen per cent less at the baseof the tower than at the top of the tower, and tends to become more nearly constant if steam is used in the` distillation. Steam will enter the base of the tower at, for example, 750 degrees Fahrenheit with a relatively large volume and leave at, for example, 300 degrees with a relatively low volume. rllhe oil vapor l enters at 7 50 degrees with relatively low volume, while at the top of the tower lighter fractions in combination with the light reflux will have a relatively large volume. Combining both the steam and oil vapors, it may be assumed that the volume at the base of the tower is f slightly less than at the top of the tower.

While this volume may 'be ten 'percent less has a lnumber of parallel elongated ports.

` i The oil ows onto the tray from connections 27 a, flows in a. uni-directionall path across the tray and down to the next tray through con- Inections 271)..Lv

` Referring to `liig.v 5, the tray 12b is equip-I i pcd with flow directing members 37, 38 and 39. As can be seen from the drawings, the oil flowing down onto the tray through the connections 27a is constrained by the directing or baille members 37 and 38 to flow to each side of the `central port 29, but cannot immediately flow along the outer ports. The oil -after Howing toeach side of the central port is caused by the baiile member39 to reverse its flow and flow backwardly inside the outermost ports and then the oil again changes its direction due to the members 37 and 38 and finally flows out through connections 276. By this means, the path ofA iow has been lengthened and t-he cross-sectional area of lflow has been diminished. The length of ltravel is approximately tripled and the velocity is consequently made more nearly equal to the velocity on the top trays 12a since the volume of liquid has been reduced to approximately one-third as shown by the diay gram, Fig. 2. i

Referring to Fig. 6, the oil enters the tray 120 from connection 27a and passes serially ,between all the ports due to the baflling members 40, 41, 42 and 43. Thus the length of the path of travel has been doubled compared with the flow over the trays 12b, and the velocity has been maintained at an appreciable value sincethe lreduction in liquid volume is substantially in accordance with the change in flow area.

Thus it will be seen that l have increased the length of the path of flow of liquid on the lower trays relative to the length of path of How on the upper trays, and diminished the cross-sectional areas, in order to equalize thel rate of liquidflow on the trays and to compensate foi` dierenceofquantity of liquid in diderent parts of the tower. l have also provided means for preventing precipitation on trays in a relatively high temperature zone.

lt may be pointed out that my invention l affords an advantage as respects adjustment of parts within *thev tower. With a tower having the same kindgof trays at all points in the tower, so that the velocity of flow is differentat different points of the tower and so that the quantiy is different at different points l of the tower, the height of liquid on the trays diers as the quantityl diers. As above stated, the level. on a tray is determined by an overflow edge orlike device.' The liquid'lias 7 a height on the tray above the overflow edge which has a relation to qiantity and velocity. ln the type of tower referred tb with equal trays throughout the tower,rthe liquid will have a higher surface level above the overow edge in the upper part of the tower than in the lower partof the tower. Consequentl it is common practice to adjust thecaps (isee cap 30, Fig. 8) over theports to a lower height on the trays in the, lower partof the tower sothat the caps will have a more or less uniform submergeuce in the liquidbody. By means of the present invention, the velocity is/equalize'd, that is, lmade uniform to a more or less extent and, preferably, toas near uniform as possible, as a result of which the level of thesurface of liquid at the overflow edges of the trays will be more uniform. Consequently, my' inventionpermits of havlt will be obvious that the invention is not confined to any specific arrangements of flowdirecting members and that it is a simple matter for any given installation to devise a set of baiies or other flow-directing means which will alter the path of flow to make the flow as near uniform or to otherwise equalize the rate of flow to any extent desired with respect to the particular installation.

What ll claim is:

1. A fractionating tower vcomprising a shell, means to supply oil vapor to the shell,

means for produclng downward flow of condensate in the shell, a plurality of bubble trays in the shell for flow of liquid thereover and for contact of the liquid with vapor,

means for withdrawing fraction products `at different levels and means on the trays for equalizing the rate of liquid flow on the trays.

2. A fractionating tower comprising a shell,.means to supply oil vapor to the shell, means for producing downward flow of condensate in the shell, a plurality of bubble trays inthe shell for How of liquid thereover and for contact of the liquid with vapor, means for withdrawing fraction products at dii'erent levels and means on` the trays for directing How of liquid thereon to compensate for di'erences of quantity of liquid in diderent parts of the tower.

3. A tractionating tower comprising a shell, means to supply oil vapor to the shell, means for producing downward flow of condensate in the shell, a plurality of bubble i' means for producingdownward lowl of contrays in the shell for How of liquid thereover and for contact of the liquid .with vapor, means for withdrawingraction products at dierenty levels and means fordecreasing the width of the path of flow. of liquid on lower trays below the width of the path of flow on upper trays.

, 4. A ractionating tower comprising a shell, neans to supply oilvapor to the shell,

densate in the shell, a plurality of bubbleV trays in the shell for ow of liquid thereover and for contact of the liquid with vapor,

means for withdrawing fraction products at different levels, means for providing a given channel of flow on bubble trays in a relatively low temperature zone and means for providing a longer and narrower channel of flow on bubble trays in the relatively high temperature zone for preventing precipitation on the latter.

5. A fractionating tower comprising a shell, means to supply oil vapor to said shell, means for producing downward low of condensate in the shell, means for withdrawing a fraction product Jfrom the shell, an upper set of trays above the point of fraction withdrawal, a lower set of trays below the point of fraction' withdrawal, the trays comprising means for contact of vapor with liquid lowing thereover and mea-ns for producing a longer. path of flow of liquid over the trays of the lower set than the trays of the upper set means for contact of vapor with liquid fiowing thereover, means for producing flow of liquid in one direction over the trays of the upper set and means for producing flow of liquid in several directions over the trays of the lower set.

7. ln a fractionating tower wherein condensate cascades downwardly over gas and liquid contact members and in Contact with upwardly flowing vapors and wherein there is intermediate `fraction withdrawal, that improvement which consists in alterin the dimensions of the path of liquid flow a ter fraction withdrawal to substantially prevent reduction of liquid flow velocity due to the withdrawal.

8. lln a .ractionating tower wherein ycondensate cascades downwardly over gas` and liquid contact members and in contact with upwardly flowing vapors and wherein 'there is intermediate fraction withdrawal, that improvement which consists in altering the dimensions of the path of liquid How after fraction withdrawal to substantially prevent re` duction 'of liquid flow velocity due to the withdrawal, while maintaining substantially constant cross-sectional area of gaspassage throuh the gas and liquid contact members. 9. fractionatingA tower comprising a shell, means to supply oil vapor to said shell, i

meansl for producing downward flow of condensate in the shell, means for withdrawing a fraction product from the shell, an upper set4 of trays above the point of fraction withdrawal, a lower set of trays below the point of fraction withdrawal, the trays having ports for passage of vapor therethrough of equal area for the lupper and lower sets of trays and members adjacent said orts for causing contact of vapor with liqui flowing thereover, and means for altering the width of the path of flow of liquid over the trays of the lower set relative to the upper set to pro vide a lesser edective cross-sectional area of path ot dow on the trays of the lower set than on thetrays of the upper set.

10. A tractionating tower comprising a shell, means to supply oil vapor to the shell, means for producing downward dow of condensate inthe shell,\ a plurality of bubble trays in the shell for dow of liquid thereover and for contact of the liquid with vapor, means for withdrawing :traction products at did'erent levels and upstanding baing members on lower trays for decreasing the cross-sectional area of dow thereover vbelow the cross-sectional area of dow on upper trays.

11. lin a fractionating tower wherein conf densate cascades downwardly over gas and Vao liquid contact members and. in contact with upwardly dowing vapors and wherein there is intermediate fraction withdrawal, that improvement which consists in providing a given path of liquid dow before fraction K withdrawal and providing a longer and narrower path of liquid dow after traction with-y drawal to substantially prevent reduction of" liquid dow Velocitydue to withdrawah 12. A fractionating tower comprising a shell, means to supply oil vapor to the shell,

' means for producing downward dow of conwhich, fraction products are withdrawn` whereby substantially the same height adjustment of bubble caps on the trays gives` substantially uniform submergence` of the caps on the trays irrespective oit the quantity of liquid dowing over the trays.

13. rllhe method of Aractionally distilling hydrocarbon yoils which comprises heating the oil tonvaporization temperature, introducing the heated oil into a tractionating tower having a plurality of bubble traysabove the oil inlet, passing vapors of the oil counter-current to and in Contact with redux oil, withdrawing redux oil at a plurality of levels in the tower and increasing the velocity of dow of redux on the trays below each point of redux withdrawal to provide a substantially uniform velocity of dow of redux oil on said trays throughout the tower,l

1l. The method of fractionally 'distilling hydrocarbon oils which comprisesheating the oil to vaporization temperature, introducing the heated oil into a tractionating tower having a plurality of bubble trays above the oil inlet, passing vapors of the `oil counter-current to and in contact with redux oil, withshell, a plurality oit bubble trays in the shell above the inlet, means for producing a downward dow of `condensate in the shell over the trays, vapor openings in the trays, walls surrounding the openings defining paths for the dow of redux over the trays, means dor withdrawing redux at diderent levels from the shell, means on the trays associated with the paths for the dow of redux arranged so that the velocity of dow of the oil vapors through the trays and the velocity of dow of the redux on the trays are substantially respectively constant throughout the tower above the said inlet, l

16. rlihe method of ractionallydistilling hydrocarbon oils which comprises heating the oil to vaporizationtemperature, introducing the heated oil into a-ractionating tower having a plurality 'of bubble trays above the oil inlet, passing vapors of the oil counter-current to and in contact with redux oil, withdrawing redux oil at a plurality oit levels invv the tower, maintaining the 'velocity of dow of the oil vapors through said trays substantially constant and increasing the velocity of dow of redux on the trays below each point of redux withdrawal to provide a substantially uniform velocity of dow ont redux oil on said trays 'throughout the tower.

lln testimony whereof ll hereunto ax my signature.

JHN SAMUEL WALLIS.

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